EP3222731A1 - Procédé de production d'éthanol - Google Patents

Procédé de production d'éthanol Download PDF

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Publication number
EP3222731A1
EP3222731A1 EP16161566.1A EP16161566A EP3222731A1 EP 3222731 A1 EP3222731 A1 EP 3222731A1 EP 16161566 A EP16161566 A EP 16161566A EP 3222731 A1 EP3222731 A1 EP 3222731A1
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EP
European Patent Office
Prior art keywords
stream
enriched
containing stream
vol
ethanol
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP16161566.1A
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German (de)
English (en)
Inventor
Gerald Sprachmann
Jacobus Johannes GEERLINGS
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
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Priority to EP16161566.1A priority Critical patent/EP3222731A1/fr
Publication of EP3222731A1 publication Critical patent/EP3222731A1/fr
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
    • C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
    • C12P7/06—Ethanol, i.e. non-beverage
    • C12P7/065—Ethanol, i.e. non-beverage with microorganisms other than yeasts
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • the present invention relates to a method of producing ethanol.
  • the present invention relates to a method of producing ethanol from a CO 2 -containing stream.
  • Several methods for producing ethanol are known in the art.
  • One or more of the above or other objects can be achieved by providing a method of producing ethanol, the method at least comprising the steps of:
  • ethanol can be produced starting from a CO 2 -containing stream, by using a combination of CO 2 reduction and bacterial fermentation.
  • a CO 2 -containing stream is provided.
  • This CO 2 -containing stream is not particularly limited and may have various origins, including waste streams.
  • An example of a suitable CO 2 -containing stream is an off-gas stream coming from Heavy Paraffin Synthesis.
  • the CO 2 -containing stream provided in step (a) comprises at least 5.0 vol.% CO 2 , preferably at least 10.0 vol.%.
  • the CO 2 -containing stream provided in step (a) comprises at most 60 vol.% CO 2 .
  • the CO 2 -containing stream provided in step (a) comprises also some CO.
  • the CO 2 -containing stream provided in step (a) comprises at least 2.0 vol.% CO, preferably at least 5.0 vol.%, more preferably at least 10.0 vol.% and typically at most 35 vol.%.
  • the CO 2 -containing stream provided in step (a) typically comprises some H 2 , such as at least 1.0 vol.% H 2 , preferably at least 2.0 vol.%, more preferably at least 5.0 vol.%.
  • the CO 2 -containing stream provided in step (a) typically comprises no O 2 or only very small amounts of O 2 , such as below 0.2 vol.% O 2 , preferably less than 0.1 vol.%, more preferably less than 0.05 vol.% or even less than 0.01 vol.%.
  • the CO 2 -containing stream provided in step (a) has been obtained from a preceding (or 'second') CO 2 -containing stream that has been subjected to a preceding (or 'second') bacterial fermentation step thereby obtaining a second ethanol-enriched liquid stream.
  • this preceding CO 2 -containing stream is referred to as 'second CO 2 -containing stream'
  • the CO 2 -containing stream provided in step (a) can be referred to as 'first CO 2 -containing stream'.
  • the preceding (or 'second') CO 2 -containing stream comprises at least 10.0 vol.% CO 2 , preferably at least 20 vol.% and typically at most 60 vol.%.
  • step (b) at least a part of the CO 2 of the CO 2 -containing stream provided in step (a) is converted, thereby obtaining a CO-enriched stream.
  • the person skilled in the art will readily understand that the conversion of the CO 2 to obtain CO can be performed in many ways. As the person skilled in the art is familiar with such conversions, this is not discussed here in detail. Examples of suitable conversions include RWGS (Reverse Water Gas Shift) reactions, electrolysis or other CO 2 reduction process.
  • RWGS Reverse Water Gas Shift
  • the conversion in step (b) is performed in the presence of hydrogen (H 2 ).
  • H 2 is present in an amount of from 20 to 60 vol.%.
  • the H 2 /CO 2 volume ratio of the CO 2 -containing stream provided in step (a) directly before it is converted in step (b) is at least 1.0, preferably at least 2.0, more preferably at least 4.0 and typically below 10.
  • the conversion in step (b) is by a Reverse Gas Shift reaction.
  • the conversion in step (b) is by electrolysis.
  • electrolysis is known per se, this is not further discussed here in detail.
  • the electrolysis is performed using Electrolytic-Based Fuel Cells.
  • the pressure during the conversion in step (b) is at least 2.0 bara, preferably at least 10 bara, more preferably at least 20 bara, even more preferably at least 40 bara and typically below 100 bara.
  • step (c) the CO-enriched stream obtained in step (b) is subjected to bacterial fermentation, thereby obtaining at least an ethanol-enriched liquid stream and a CO 2 -enriched gaseous stream.
  • the bacterial fermentation is not particularly limited and may be performed in various ways. As the person skilled in the art is familiar with bacterial fermentation, this is not discussed here in detail. Examples of suitable bacterial fermentations include gas fermentation processes as available from LanzaTech (Skokie, Illinois (USA)), Ineos (Rolle, Switzerland) and Coskata (Warrenville, Illinois (USA)). Preferably the bacterial fermentation is performed by at least one member of the Carboxydotrophic bacteria such as Clostridium autoethanogenum.
  • the bacterial fermentation of step (c) takes place at pressure of between 1 and 100 bara and temperatures of 5 to 100°C.
  • the bacterial fermentation in step (c) takes place at pressure of at least 2.0 bara, preferably at least 10 bara, more preferably at least 20 bara, even more preferably at least 40 bara.
  • the same pressure and temperature ranges would typically be selected (although the actual conditions of the first and second bacterial fermentation may differ).
  • the ethanol-enriched liquid stream and CO 2 -enriched gaseous stream obtained in step (c) can be further processed if needed.
  • the liquid ethanol-enriched stream will be distilled, preferably together with the second ethanol-enriched liquid stream (if any). Thereafter, the distilled ethanol stream may be used as such, blended with other streams or further reacted to other products.
  • the CO-enriched stream obtained in step (b) is separated to obtain a H 2 -enriched stream (preferably containing from 50 to 99 vol.% H 2 ).
  • This separation can for example be performed in a pressure-swing adsorption (PSA) device or using a H 2 -selective membrane.
  • PSA pressure-swing adsorption
  • H 2 -selective membrane preferably containing from 50 to 99 vol.% H 2 .
  • at least a part of the H 2 -enriched stream is reused in the conversion in step (b).
  • the H 2 -enriched stream may directly be sent to the reactor in which the conversion of step (b) takes place.
  • the H 2 -enriched stream may first be combined with the CO 2 -containing stream provided in step (a).
  • a H 2 -makeup stream may be required.
  • such a H 2 -makeup stream is produced using renewable power resources (biomass, H 2 O hydrolysis using renewable power).
  • FIG. 1 shows a process block scheme, generally referred to with reference number 1, for a method of producing ethanol.
  • the process block scheme shows a first reactor 2 for converting CO 2 into CO (in the embodiment of Figure 1 , using a Reverse Water Gas Shift reaction), a second reactor 3 (for performing bacterial fermentation) and a separator 4 (such as a Pressure-Swing Adsorption device) for removing H 2 .
  • a first reactor 2 for converting CO 2 into CO in the embodiment of Figure 1 , using a Reverse Water Gas Shift reaction
  • a second reactor 3 for performing bacterial fermentation
  • a separator 4 such as a Pressure-Swing Adsorption device
  • a CO 2 -containing stream 10 is provided (e.g. obtained from a Heavy Paraffin Synthesis process) and sent to the RWGS reactor 2.
  • a CO-enriched stream 20 is obtained.
  • a H 2 recycle stream 50 obtained from the separator 4
  • a H 2 make-up stream 70 are used to supply H 2 to the RWGS reactor 2.
  • the CO-enriched stream 20 is subjected in reactor 3 to bacterial fermentation, thereby obtaining an ethanol-enriched liquid stream 30 and a CO 2 -enriched gaseous stream 40.
  • the ethanol-enriched liquid stream 30 may be further processed as desired.
  • the CO 2 -enriched gaseous stream 40 is separated in separator 4 to obtain a H 2 -enriched stream 45, which is used as a H 2 recycle stream in the RWGS reactor 2.
  • the CO-enriched stream 20 may be separated (not shown) to obtain an H 2 -enriched stream 50 (showed as a dashed line in Figure 1 ) and recycled to just upstream of the reactor 2.
  • Figure 2 shows a variation of the process of Figure 1 , wherein the CO 2 -containing stream 10 has been obtained from a preceding CO 2 -containing stream 80 that has been subjected to a preceding bacterial fermentation in reactor 5 thereby obtaining a second ethanol-enriched liquid stream 90 and the CO 2 -containing stream 10.
  • FIG 3 shows an alternative to the processes of Figs 1 and 2 , wherein a CO 2 electrolysis step takes place in reactor 2. Rather than a separation (as done in separator 4 of Figs 1 and 2 ), in the embodiment of Figure 3 , the CO 2 -enriched gaseous stream 40 is split and part of it is recycled as stream 45 to just upstream of the CO 2 electrolysis reactor 2 and combined with the CO 2 -containing stream 10.
  • the CO 2 electrolysis reactor 2 uses renewable power.
  • CO-enriched stream 20 may be separated (not shown) to obtain an H 2 -enriched stream 50 (showed as a dashed line in Figure 3 ) and recycled to just upstream of the CO 2 electrolysis reactor 2.
  • Figure 4 shows an alternative to the processes of Figs 1 and 2 , wherein a H 2 -separation step occurs in separator 4 before the bacterial fermentation in reactor 3.
  • the H 2 -recycle stream 50 (obtained from the separator 4) is reused in the conversion in reactor 2, by combining it with the CO 2 -containing stream 10 and H 2 make-up stream 70.
  • Table 1 provides the conditions and the compositions of the various streams as mentioned in respect of the line-up of Fig. 4 .
  • Clostridium autoethanogenum was used.
  • Table 1 10 20 20' 30 40 50 70 CONDITIONS T [°C] 700-900 40 40 40 40 40 40 40 p [bara] 52 52 52 52 52 52 52 52 COMPONENTS [vol.%] H 2 56.5 48.2 8.5 - 8.3 99.0 100 CO 7.3 15.6 27.6 - 6.0 - - CO 2 14.1 5.8 10.2 - 27.0 - - O 2 - - - - - - - N 2 4.9 4.9 8.7 - 9.4 0.9 - Argon 0.7 0.7 1.2 - 1.3 - - H 2 0 - - - 82.2 - - - Methane 16.5 24.8 43.8 - 48.0 0.1 - Acetic Acid - - - 0.3 - - - Ethanol - -
  • the present invention provides a method for producing ethanol from a CO 2 -containing stream.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Zoology (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Microbiology (AREA)
  • Biotechnology (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Biochemistry (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
EP16161566.1A 2016-03-22 2016-03-22 Procédé de production d'éthanol Withdrawn EP3222731A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP16161566.1A EP3222731A1 (fr) 2016-03-22 2016-03-22 Procédé de production d'éthanol

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Application Number Priority Date Filing Date Title
EP16161566.1A EP3222731A1 (fr) 2016-03-22 2016-03-22 Procédé de production d'éthanol

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EP3222731A1 true EP3222731A1 (fr) 2017-09-27

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2017136478A1 (fr) 2016-02-01 2017-08-10 Lanzatech New Zealand Limited Procédé intégré de fermentation et d'électrolyse
JP2021512598A (ja) * 2018-02-12 2021-05-20 ランザテク，インコーポレイテッド 炭素変換効率を改善するためのプロセス

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009010347A2 (fr) * 2007-07-19 2009-01-22 Ineos Europe Limited Procédé de production d'alcools
WO2012054798A2 (fr) * 2010-10-22 2012-04-26 Lanzatech New Zealand Limited Procédés et systèmes pour produire des produits hydrocarbonés

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009010347A2 (fr) * 2007-07-19 2009-01-22 Ineos Europe Limited Procédé de production d'alcools
WO2012054798A2 (fr) * 2010-10-22 2012-04-26 Lanzatech New Zealand Limited Procédés et systèmes pour produire des produits hydrocarbonés

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
KLASSON K T ET AL: "Bioconversion of synthesis gas into liquid or gaseous fuels", ENZYME AND MICROBIAL TECHNOLOGY, STONEHAM, MA, US, vol. 14, no. 8, 1 August 1992 (1992-08-01), pages 602 - 608, XP023679463, ISSN: 0141-0229, [retrieved on 19920801], DOI: 10.1016/0141-0229(92)90033-K *
YOUSSEF REDISSI ET AL: "Valorization of Carbon Dioxide by Co-Electrolysis of CO2/H2O at High Temperature for Syngas Production", ENERGY PROCEDIA, vol. 37, 1 January 2013 (2013-01-01), NL, pages 6667 - 6678, XP055298872, ISSN: 1876-6102, DOI: 10.1016/j.egypro.2013.06.599 *

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2017136478A1 (fr) 2016-02-01 2017-08-10 Lanzatech New Zealand Limited Procédé intégré de fermentation et d'électrolyse
EP3411489A4 (fr) * 2016-02-01 2020-01-15 Lanzatech New Zealand Limited Procédé intégré de fermentation et d'électrolyse
EP4234707A3 (fr) * 2016-02-01 2024-06-05 LanzaTech NZ, Inc. Procédé intégré de fermentation et d'électrolyse
JP2021512598A (ja) * 2018-02-12 2021-05-20 ランザテク，インコーポレイテッド 炭素変換効率を改善するためのプロセス
US11359294B2 (en) * 2018-02-12 2022-06-14 Lanzatech, Inc. Process for improving carbon conversion efficiency

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